CN115043701A - Preparation method of cis-1-chloro-3, 3, 3-trifluoropropene - Google Patents
Preparation method of cis-1-chloro-3, 3, 3-trifluoropropene Download PDFInfo
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- C07C17/25—Preparation of halogenated hydrocarbons by splitting-off hydrogen halides from halogenated hydrocarbons
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- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/20—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms
- C07C17/202—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction
- C07C17/206—Preparation of halogenated hydrocarbons by replacement by halogens of halogen atoms by other halogen atoms two or more compounds being involved in the reaction the other compound being HX
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- C07C17/35—Preparation of halogenated hydrocarbons by reactions not affecting the number of carbon or of halogen atoms in the reaction
- C07C17/358—Preparation of halogenated hydrocarbons by reactions not affecting the number of carbon or of halogen atoms in the reaction by isomerisation
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- C07C17/383—Separation; Purification; Stabilisation; Use of additives by distillation
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Abstract
A preparation method of cis-1-chloro-3, 3, 3-trifluoropropene belongs to the technical field of fluorine chemistry, and comprises the steps of reacting R240fa with HF to generate cis-1-chloro-3, 3, 3-trifluoropropene and trans-1-chloro-3, 3, 3-trifluoropropene, and isomerizing the trans-1-chloro-3, 3, 3-trifluoropropene in an isomerizer after preheating to generate the cis-1-chloro-3, 3, 3-trifluoropropene, and is characterized in that the isomerization process conditions are as follows: the catalyst is an alumina pellet catalyst loaded with chromium chloride, the isomerization temperature is 350-400 ℃, and the pressure is 0.1-0.3 MPa. Compared with the prior art, the method is suitable for industrial mass production, and the isomerization selectivity and the conversion rate of the method are obviously superior to those of the prior art.
Description
Technical Field
The invention belongs to the technical field of fluorine chemistry, and particularly relates to a preparation method of cis-1-chloro-3, 3, 3-trifluoropropene.
Background
1-chloro-3, 3, 3-trifluoropropene (HCFO-1233 zd) is an excellent ODS substitute, can be used for foaming agent, refrigerant, cleaning agent, heat transfer medium and the like, and has a good development prospect.
The synthesis and application of HCFO-1233zd (E) (organic fluorine industry, Qizhonglongyan e, etc.; stage 2 of 2015) reviewed three processes for the separate synthesis or co-production of HCFO-1233zd (E) by gas-liquid method, and analyzed the application thereof relatively comprehensively.
The trend of the replacement technology of hydrochlorofluorocarbon in the cleaning industry (Hill. Ling Jingling Lin Ling, Zhejiang chemical industry, 2016, vol. 47, No. 7) records that trans-1-chloro-3, 3, 3-trifluoropropene is used in cleaning agent, and has the disadvantages of low boiling point, high unit price, etc.
The progress of HCFO-1233zd and HCFO-1336mzz (Z) preparation and use (Guangzhou chemistry, volume 45, No. 3, No. 2020, 6 of Korean plum, et al) describes the production of HCFO-1233zd by Aroma France, Hounwell International, and Asahi glass company, Japan, and describes the advantages and disadvantages of these methods.
Statistical analysis of the technical development of HCFO-1233zd from the perspective of our national patent literature was performed in the national patent analysis of HCFO-1233zd refrigerant (Geng Leyin scientific Innovation and application (27 of 2019)), and the patents referred to therein are incorporated herein by reference in their entirety.
Chinese patent publication No. CN109627143A discloses a method for preparing trans-1-chloro-3, 3, 3-trifluoropropene, which is characterized in that: cis-1-chloro-3, 3, 3-trifluoropropene is used as a raw material, and the E-HCFC-1233zd is generated by gas phase catalytic isomerization at 50-300 ℃ in the presence of a fluorination catalyst and in the presence or absence of a diluent gas.
Chinese patent publication No. CN111925273A discloses a method for producing high-purity cis-1-chloro-3, 3, 3-trifluoropropene, which comprises subjecting a mixed gas generated by fluorination of 1,1,1,3, 3-pentachloropropane to separation and purification to obtain trans-1-chloro-3, 3, 3-trifluoropropene, then subjecting the mixed gas to catalytic isomerization reaction to obtain cis-trans mixed product, and further separating and purifying to obtain high-purity cis product. In the scheme, the chiral conversion adopts an isomerization catalyst which is aluminum chlorofluoride, magnesium oxychloride, chromium oxychloride and chromium oxychloride; the isomerization reaction conditions are as follows: in the presence of an isomerization catalyst, the reaction pressure is 0.01-0.5MPa, the reaction temperature is 150-350 ℃, and the contact time is 20-100 s; the preferred isomerization temperature is 200-300 ℃.
Chinese patent publication No. CN108383679A discloses a co-production method of trans-1-chloro-3, 3, 3-trifluoropropene and 2,3,3, 3-tetrafluoropropene, wherein 1,1,1,3, 3-pentachloropropane and 1,1,1,2, 3-pentachloropropane are mixed in proportion and then are introduced into a first reactor together with hydrogen fluoride, fluorination reaction is carried out under the action of a catalyst A to obtain trans-1-chloro-3, 3, 3-trifluoropropene, cis-1-chloro-3, 3, 3-trifluoropropene, 2-chloro-3, 3, 3-trifluoropropene, hydrogen chloride and hydrogen fluoride, the trans-1-chloro-3 is obtained by directly entering a second reactor without separation and reacting under the action of a catalyst B, 3, 3-trifluoropropene, 2,3,3, 3-tetrafluoropropene, hydrogen chloride and hydrogen fluoride, and separating to obtain the products of trans-1-chloro-3, 3, 3-trifluoropropene and 2,3,3, 3-tetrafluoropropene.
Chinese patent publication No. CN108473398A discloses a method for efficiently producing 1-chloro-3, 3, 3-trifluoropropene from an intermediate product having low reactivity. Disclosed is a method for producing trans-1-chloro-3, 3, 3-trifluoropropene, which is characterized by reacting a halogenated hydrocarbon compound having 3 carbon atoms represented by the general formula (1) with hydrogen fluoride in a gas phase in the presence of a solid catalyst and chlorine gas. C 3 H X Cl Y F Z (1) (wherein X is 2 or 3, when X is 2, Y is an integer of 1 to 4, Z is an integer of 0 to 3, and Y + Z is 4. when X is 3, Y is an integer of 1 to 5, Z is an integer of 0 to 4, and Y + Z is 5), wherein the general formula (1) represents a halogenated hydrocarbon compound having 3 carbon atoms other than trans-1-chloro-3, 3, 3-trifluoropropene).
Chinese patent publication No. CN107892642A discloses an integrated process for the co-production of trans-1-chloro-3, 3, 3-trifluoropropene (1233 zd (e)), trans-1, 3,3, 3-tetrafluoropropene (1234 ze (e)), and 1,1,1,3, 3-pentafluoropropane (245 fa). The co-production is generally a three-step process. The chemical process involves the steps of: (1) reacting 240fa with excess anhydrous HF in a liquid phase catalytic reactor in such a manner as to produce primarily 1233zd (e) and 244fa (plus byproduct HCl) in combination; (2) the 244fa stream is then used to directly produce any of the three desired products; (3a) the 244fa stream can be dehydrochlorinated to produce a desired second product 1234ze (e); and/or (3b) if more 1233zd (e) product is desired, the 244fa stream can be dehydrofluorinated to produce 1233zd (e); and/or (3c) the 244fa stream can be further fluorinated to form 245 fa.
Also described in the examples of WO2008/030443 are trans R-1234ze (l, 3,3, 3-tetrafluoroformaldehyde) to cis R-1234ze using milled chromia gel pellet catalysts.
The applicants have provided as much journal and patent literature as possible in connection with the present invention, the entire contents of which are incorporated herein by reference.
By literature search, in the prior art and in the near field, isomerization is usually carried out over a catalyst, which is generally a metal chloride.
Disclosure of Invention
The invention provides a preparation method of cis-1-chloro-3, 3, 3-trifluoropropene, and the prepared cis-1-chloro-3, 3, 3-trifluoropropene is used as a cleaning agent or a complex of the cleaning agent.
The invention specifically adopts the technical scheme that:
a preparation method of cis-1-chloro-3, 3, 3-trifluoropropene is characterized by comprising the following steps:
1) the raw material R240fa and the excessive AHF are mixed in the pipeline and then enter a vaporizer, so that the mixed material initially reaches a vaporization state;
2) the vaporized materials are subjected to primary heat exchange through a tube pass of a heat exchanger, then enter a preheater to heat the materials to 300 ℃ and then enter a reactor to perform gas phase reaction;
3) the reaction product enters a cooler for cooling, then enters an HCl tower, the product at the top of the tower is cooled and then enters an acid making system to absorb HCl, the product at the bottom of the tower is sent out from a tower kettle to a deep cooler, HF separated by the deep cooler is sent to an HF circulation tank to be mixed with newly supplemented HF and then enters a vaporizer, and the organic material separated by the deep cooler enters a crude product tank;
4) conveying the materials in the crude product groove to a crude separation tower, and removing light components at the top of the tower to a water washing tower of an R245fa device; feeding the tower bottom material of the rough separation tower into a first washing tower;
5) heating and isomerizing R1233zd (E) from an R245fa device, then feeding the heated and isomerized R1233zd (E) into a first water scrubber, washing the water scrubbed and alkali-washed with a crude component tower bottom material, then feeding the washed water scrubbed and alkali-washed R1233zd (Z) into a first rectifying tower system for rectification, obtaining R1233zd (E) and R1233zd (Z) finished products at the tower top of the first rectifying tower system, and obtaining a heavy component and a R1233zd (Z) crude product at the tower bottom;
wherein the isomerization process conditions are as follows: the catalyst is an alumina pellet catalyst loaded with chromium chloride, the isomerization temperature is 350-400 ℃, and the pressure is 0.1-0.3 MPa.
Wherein the loading amount of the chromium chloride is 0.01-0.1 percent of the total weight of the catalyst.
6) The R245fa device comprises a liquid phase fluorination device, an HCl rectifying tower, a second water washing tower, a second alkali washing tower, a crude product tank and a rectifying tower, the R1233zd (Z) crude product and the excessive liquid chlorine in the step 5) enter the liquid phase fluorination device, then are rectified by the HCl rectifying tower, washed by the second water washing tower and alkali washed by the second alkali washing tower, enter the second rectifying tower system for rectification, R1234zd (E) and R245fa are obtained at the top of the tower, and heavy components are obtained at the bottom of the tower.
Wherein, the amount ratio of HF to R240fa in the step 1) is 8-12: 1; the vaporizer outlet temperature is greater than 110 c and the preferred outlet temperature is 120 c.
In the steps 2 and 3), the reacted product enters a shell side of a heat exchanger and then enters a cooler; the reactor and the preheater adopt a series connection heat conduction oil heating mode;
wherein, the HCl tower is directly cooled by a refrigerant at the temperature of-35 ℃;
wherein, cis-1233 zd and trans-1233 zd are enriched to 99.5% at the top of the first rectifying tower system, and are removed from the adsorption tower to remove trace HF and moisture, and are collected into a finished product tank after being cooled by an external condenser.
In the invention, R240fa is the abbreviation of 1,1,1,3, 3-pentachloroacetic acid; AHF is the abbreviation of anhydrous hydrogen fluoride; r245fa is an abbreviation for 1,1,1,3, 3-pentafluoropropane.
In the invention, the first rectifying tower system and the second rectifying tower system are rectifying systems consisting of a plurality of rectifying towers.
Compared with the prior art, the invention has the advantages that:
1) the invention can co-produce cis-R1233 zd, trans-R1233 zd, trans-R1234 ze and R245fa, and is very suitable for industrial mass production;
2) the isomerization catalyst of the invention has good selectivity and conversion rate.
Drawings
FIG. 1 is a block diagram of the R1233zd process flow of the present invention;
FIG. 2 is a block diagram of the R245fa process flow of the present invention.
Detailed Description
EXAMPLE 1 (best mode)
Step 1): as shown in fig. 1, the raw material R240fa and the excess AHF are mixed in the pipeline and then enter the vaporizer 1, so that the mixed material initially reaches a vaporized state; the ratio of the amount of AHF to R240fa species was 10: 1; the vaporizer outlet temperature was 120 ℃.
Step 2): the vaporized materials are subjected to primary heat exchange through a tube pass of a heat exchanger, then enter a preheater to heat the materials to 300 ℃ and then enter a reactor 2 to perform gas phase reaction; (Heat exchanger and preheater not shown in the figure)
Step 3): the reaction product enters a cooler 3 for cooling, then enters an HCl tower 4, the top product of the HCl tower 4 is cooled and then enters an acid making system to absorb HCl, the bottom product of the tower is sent out from the tower kettle to a chiller 5, AHF separated by the chiller 5 is sent to an AHF circulation tank to be mixed with newly supplemented AHF, then the mixture enters a vaporizer, and the organic material separated by the chiller 5 enters a crude product tank (not marked in the figure);
step 4): conveying the materials in the crude product tank to a coarse separation tower, wherein the number of the coarse separation tower is two, namely a first coarse separation tower 61 and a second coarse separation tower 62, and extracting light components at the top of the coarse separation tower to a second water washing tower 17 of an R245fa device (a device shown in figure 2); feeding the material at the bottom of the rough separation tower into a first washing tower 7;
step 5): r1233zd (E) from the R245fa unit enters the material heating unit 11 and then enters the isomerizer 12, the isomerizer 12 can adopt a fluidized bed type structure, the catalyst is an alumina pellet catalyst loaded with chromium chloride, the dosage of the chromium chloride is 0.05 percent of the total weight of the catalyst, the isomerization temperature is 370 ℃, the pressure is 0.2MPa, and the reactor is internally provided with excessive AHF.
Step 6): the isomerized material firstly enters a condenser 13, is condensed and then enters a first water scrubber 7, enters a first alkaline washing tower 8 after being washed with a crude component tower bottom material, and then enters a first rectifying tower system for rectification, the first rectifying tower comprises four rectifying towers which are respectively called as a tower 101, a tower 102, a tower 103 and a tower 104, wherein R1233zd (E) is extracted from the top of the tower 101, R1233zd (Z) is extracted from the top of the tower 104, heavy components are burned from the bottoms of the towers 102 and 104, and light components are recycled or burned from the top of the tower 103.
Step 7): as shown in fig. 2, the AHF, the liquid chlorine and the crude product R1233zd (Z) from the second rectifying tower system enter the liquid phase fluorination device 14, then enter the HCl rectifying tower 15 for rectification, the HCl extracted from the tower top absorbs the acid, then enter the AHF rectifying tower 16 for rectification, and the extracted AHF is recycled to the liquid phase fluorination device 14;
step 8): the material after AHF rectification enters a second water washing tower firstly, and the light components from the top of the tower of the rough separation tower are washed by water to obtain hydrofluoric acid, and then enter a second alkali washing tower 18 for alkali washing to obtain a crude product, and the crude product is stored in a crude product groove 19;
and (3) rectifying the crude product in the crude product tank 19 in a second rectifying tower system, wherein the second rectifying tower system comprises five towers which are respectively called as a tower 191, a tower 192, a tower 193, a tower 194 and a tower 195, and the five second rectifying tower systems are sequentially rectified, wherein R1233zd (Z) is obtained at the top of the tower 194, the crude product is sent to a liquid phase fluorination device 14, R1234ze (E) finished product is obtained at the top of the tower 194, and R245fa finished product is obtained at the top of the tower 195.
Example 2
The rest steps are the same as the embodiment except for the step 1) and the step 3) as follows:
step 1): as shown in fig. 1, the raw material R240fa and the excess AHF are mixed in the pipeline and then enter the vaporizer 1, so that the mixed material initially reaches a vaporized state; the ratio of the amount of AHF to R240fa species was 10: 1; the vaporizer outlet temperature was 110 ℃.
Step 5): r1233zd (E) from the R245fa unit enters the material heating unit 11 and then enters the isomerizer 12, the isomerizer 12 can adopt a fluidized bed type structure, the catalyst is an alumina pellet catalyst loaded with chromium chloride, the dosage of the chromium chloride is 0.1 percent of the total weight of the catalyst, the isomerization temperature is 350 ℃, the pressure is 0.3MPa, and the reactor is internally provided with excessive AHF.
Example 3
The rest steps are the same as the embodiment except for the step 1) and the step 3) as follows:
step 1): as shown in fig. 1, the raw material R240fa and the excess AHF are mixed in the pipeline and then enter the vaporizer 1, so that the mixed material initially reaches a vaporized state; the ratio of the amount of AHF to R240fa species was 12: 1; the vaporizer outlet temperature was 130 ℃.
Step 5): r1233zd (E) from the R245fa unit enters the material heating unit 11 and then enters the isomerizer 12, the isomerizer 12 can adopt a fluidized bed type structure, the catalyst is an alumina pellet catalyst loaded with chromium chloride, wherein the dosage of the chromium chloride is 0.01 percent of the total weight of the catalyst, the isomerization temperature is 400 ℃, the pressure is 0.1MPa, and the reactor is internally provided with excessive AHF.
Comparative example 1
The process flow is the same as the best example, except that in the isomerizer 12, the aluminum chloride catalyst is loaded, and the rest of the process conditions are the same.
Comparative example 2
The process flow is the same as in the preferred embodiment except that chromium fluoride oxide catalyst is supported in the isomerization unit 12 and the remaining process conditions are the same.
Comparative example 3
The process flow is the same as in the preferred embodiment except that in the isomerization unit 12, the zinc-supported chromium oxide catalyst is used and the remaining process conditions are the same.
Comparative examples 1-3 are catalysts commonly used in the prior art.
The comparative results are as follows:
| conversion rate | Selectivity ratio | |
| Example 1 | 52.2% | 99% |
| Example 2 | 52.1% | 99% |
| Example 3 | 52.0% | 99% |
| Comparative example 1 | 45.6% | 90% |
| Comparative example 2 | 50.5% | 99% |
| Comparative example 3 | 48.8% | 92% |
Claims (7)
1. A preparation method of cis-1-chloro-3, 3, 3-trifluoropropene comprises the steps of reacting R240fa with HF to generate cis-1-chloro-3, 3, 3-trifluoropropene and trans-1-chloro-3, 3, 3-trifluoropropene, isomerizing the trans-1-chloro-3, 3, 3-trifluoropropene in an isomerizer after preheating to generate the cis-1-chloro-3, 3, 3-trifluoropropene, and is characterized in that the isomerization process conditions are as follows: the catalyst is an alumina pellet catalyst loaded with chromium chloride, the isomerization temperature is 350-400 ℃, and the pressure is 0.1-0.3 MPa.
2. The process for producing cis-1-chloro-3, 3, 3-trifluoropropene according to claim 1, wherein the weight of chromium chloride is 0.01 to 0.1% of the total weight of the catalyst.
3. The process for producing cis-1-chloro-3, 3, 3-trifluoropropene according to claim 1, which comprises the steps of:
1) mixing the raw material R240fa with excessive AHF, and introducing into a vaporizer to preliminarily vaporize the mixed material;
2) the vaporized materials are subjected to primary heat exchange through a tube pass of a heat exchanger, then enter a preheater to heat the materials to 300 ℃ and then enter a reactor to perform gas phase reaction;
3) the reaction product enters a cooler for cooling, then enters an HCl tower, the tower top product is cooled and then enters an acid making system to absorb HCl, the tower bottom product is sent out from the tower kettle to a chiller, HF separated by the chiller is sent to an HF circulation tank to be mixed with newly supplemented HF and then enters a vaporizer, and the organic material separated by the chiller enters a crude product tank;
4) conveying the materials in the crude product groove to a crude separation tower, and removing light components at the top of the tower to a water washing tower of an R245fa device; feeding the tower bottom material of the rough separation tower into a first washing tower;
5) heating and isomerizing R1233zd (E) from an R245fa device, then feeding the heated and isomerized R1233zd (E) into a first water scrubber, washing the water scrubbed and alkali-washed with the materials at the bottom of a crude separation tower, and then feeding the washed and alkali-washed materials into a first rectifying tower system for rectification, thus obtaining R1233zd (E) and R1233zd (Z) finished products at the top of the first rectifying tower system, and obtaining heavy components and R1233zd (Z) crude products at the bottom of the tower;
6) the R245fa device comprises a liquid phase fluorination device, an HCl rectifying tower, a second water washing tower, a second alkali washing tower, a crude product tank and a rectifying tower, the R1233zd (Z) crude product and liquid chlorine in the step 5) enter the liquid phase fluorination device, then are rectified by the HCl rectifying tower, washed by the second water washing tower and alkali washed by the second alkali washing tower, enter the second rectifying tower system for rectification, R1234zd (E) and R245fa are obtained at the top of the tower, and heavy components are obtained at the bottom of the tower.
4. The process according to claim 3, wherein the ratio of HF to R240fa in the step 1) is 8 to 12: 1; the vaporizer outlet temperature is greater than 110 ℃.
5. The process for producing cis-1-chloro-3, 3, 3-trifluoropropene according to claim 4, wherein the vaporizer outlet temperature is 120 ℃.
6. The process according to claim 3, wherein in the step 2 or 3), the reaction product is introduced into the shell side of a heat exchanger and then into a cooler.
7. The process for preparing cis-1-chloro-3, 3, 3-trifluoropropene according to claim 3, wherein cis-1233 zd and trans-1233 zd are enriched to more than 99.8% at the top of the first rectifying column system, and then are removed from the adsorption column to remove trace amounts of HF and moisture, and are condensed by an external condenser and collected into a finished product tank.
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